Regenerative furnace for manufacture of acetylene by pyrolysis



y 1943- R. 1.. HASCHE ETAL 2,313,688

REGENERATIVE FURNACE FOR MANUFACTURE OF AGETYLENE BY PYROLYSIS Filed Sept. 18, 1941 s Sheets-Sheet 1 AIR STACK Fig.1.

FUEL GAS kw (IDMBUSTION CHAMBER STEAM PURGE WATER 28 22? vclwuep GAS ,1 21

SEAL BOX 1 DILUENI PROCESS GAS a woe/rm Willi/Om B. Hm 77-21- PM SW11, I

Y 4 R. HASCHE ETAL 2,318,688

REGENERATIVE FURNACE FOR MANUFACTURE OF ACETYLENE BY PYROLYSIS Filed Sept. 18, 1941 3 Sheets-Sheet 2 F Z HYDRAULICALLY bg OPERATED VALVE WATER- COOLED CRACKED GAS SEAL BOX HYDRAULICALLY OPERATED VALVE REFRACTORY FLUI! GAS TO STACK COMBUSTION c c m STACK VALVE CHAMBER CHAMBER y 1943- R. L. HASCHE El'AL 2,318,688

REGENERATIVE FURNACE FOR MANUFACTURE OF ACETYLENE BY PYROLYSIS Filed'se t. 18, 1941 3 Sheets-Sheet s FLQ 4 :REFRACTORY PA SS AGEWP YS RE FRACTORY PA SSAG EWAY G W W L F Y A w E G A CS TP J 0 \I if)? G m w 0 w H m U THICKNESS OF REFRACTORY Rudolph Leonard HaAche William B.H'Lncke INVENTORS ATTO NEYS Patented May 11, 1943 REGENERATIVEFURNACE FOR MANUFAC- v TUBE F ACETYLENE BY PYROLYBIS Rudolph Leonard Hasche' and William B. Hincke;

Kingsport, Tenn, asslrnors to Eastman Kodak Company, Rochester, N. Y., a corporation of v New Jersey A Application September is, 1941", Serial No. 411,418

6Claims. (Cl. 23-217 This invention relates .to processes and apparatus for obtaining rapid heat input and with-' drawal at high temperatures without apparatus destruction, andparticularly to process and apparatus for manufacturing acetylene by the pyrolysis of hydrocarbons. More particularly this invention concerns a pyrolysis or cracking treatment carried out in a specially constructed regenerative, heat and make, or similar type of apparatus operated by novel procedure wherein high yields of acetylene, and other advantages, may be obtained.

We have found an efficient method and apparatus for the manufacture of acetylene from hydroc arbons wherein the pyrolysis treatment is ob ined from heat stored in refractory surfaces,

oviding certain procedure is followed and the /apparatus constructions employed described in regenerative type of heating apparatus which This application is a continuation-in-part of our application Ser. No. 259,198, flied March 1, 1939.

In the industries, acetylene has beenproduced from calcium carbide but this is a rather expensive procedure. It has been proposed to produce acetylene by other methods, such asby the pyrolysis of hydrocarbons. Acetylene, however, is somewhat unstable,tends to polymerize, or become over-cracked, or otherwise presents problems in production. While acetylene may be successfully produced in externally heated tubes, there are certain conditions 'under which it is desirable to provide a different apparatus and method for manufacturing acetylene from hydrocarbons, as for example, non-availability of large tubes, special installation problems, installation of large ,uhits and other conditions.

The regenerative type furnace is quite old and has been used for many years in the manufacture of illuminating gas, carbon black, hydrogen, and more recently in the manufacture of aromatic hydrocarbons. Although the regenerative type furnace hasbeen employed for the aforementioned purposes, its use for the pyrolysis of hydrocarbons to acetylene has been limited and the results not particularly satisfactory. After considerable investigation, we have found various respects wherein prior art type of regenerative apparatus was not satisfactory for acetylene manufacture and otherwise discovered disadvantages possessed by prior art equipment.

We have found that by certain marked departures, as will be described in detail hereinafter, in the construction of the regenerative type equipment, suitable apparatus for acetylene manufacture, and other purposes, may be obtional practice.

detail hereinafter.

This invention has for one object to provide a will withstand high rates of heat input and withdrawal at high temperatures and is particularly adapted for processing hydrocarbons to obtain acetylene therefrom. Still another object'is to provide a regenerative type furnace which includes features ofconstruction involving a substantial departure from conventional regenerative furnaces. Another object is to provide a regenerative'furnace wherein hydrocarbon materials may be raised to 1200-( in a relatively short period of time, of the order of a fraction of a second. Still another object is to provide a regenerative furnace? construction wherein there are certain definite ratios between the heating surfaces and the heating spaces, as will be described in detail hereinafter.

Still another object is to provide a pyrolysis process particularly adapted for manufacturing acetylene from non-acetylenic hydrocarbons, wherein the pyrolysis heating is obtained from the heat stored in refractory masses. Still another object is to provide a pyrolysis process for converting saturated hydrocarbons to unsaturated hydrocarbons such as acetylene with a minimum of carbon. monoxide and carbon dioxide formation, even though regenerative heating is employed in the pyrolysis. A still further object is to provide a novel method, for operating a regenerative cracking furnace employed in manufacturing acetylene containing gas from hydrocarbon materials. pear hereinafter. 1

In our investigation, we have developed certain information which is discussed below, inasmuch as it is believed such discussions will aid in a better understanding of our novel process and apparatus. a

In the high temperature pyrolysis of hydrocarbon materials for the production of acetylene, a

large number of competing reactions take place.

The simplest reaction and apparently the predominating one at temperatures of '1000' C. is substantially complete decomposition of the hydrocarbon to the elements hydrogen and carbon. If water vapor or steam, or catalytic materials such as for example nickel, are present, water gas Other objects will ap-,

reaction products as carbon monoxide, carbon dioxide, water, and hydrogenmay result.

Inasmuch as in the prior art the first reaction was desired, namely, .the decomposition of the hydrocarbon into carbon black and hydrogen, for example, regenerative furnaces were filled with refractory checker-brick more or less miscellaneously cross-piled or positioned within the apparatus. Since the object in the prior art regenerative furnace was merely to'delay the passage of the hydrocarbons until they had obtained temperatures in excess of 1000 C. and become decomposed to carbon and hydrogen, various simplified baflling arrangements functioned satisfactorily. In such prior art constructions refractory several inches in thickness was frequently employed with a flue space the same size as the refractory. Therefore, the ratio in such construction is 1:1. This matter of ratio will be discussed in greater detail hereinafter.

In the employment of regenerative furnaces that a number of factors should be taken intoconsideration and controlled as follows:

First, the maximum temperature to which the hydrocarbon and/or other materials are to be heated;

Second, the time required for the hydrocarbon to obtain thistemperature;

Third, the residence time that the gas is at this temperature and the rapidity with which it is cooled; and

Fourth, the materials from which the regenerative heating elements are constructed.

After considerable investigation, we have found that by the use of the construction described in detail hereinafter, a regenerative furnace and process highly satisfactory for use in manufacturing acetylene from hydrocarbon materials was obtained. In our regenerative furnace it is readily possible to operate within the following standards: (1) the maximum temperature to which the. hydrocarbon and diluent mixture heated is between approximately 1200 C. and 1600 C., (2) the time interval required for the hydrocarbon-diluent to attain such a temperature is less than 0.20 second in the range from 700 C. to the maximum, (3) the time interval that the acetylene containing gas can be maintained at the high temperatures before quenching to below 400 C. is less than approximately 0.20 second, (4) the materials from which the heat storing and heat transferring elements are constructed have the following properties (a) as nearly non-catalytic as possible to the undesirable decomposition reactions such as the formation of carbon black, etc., (b) refractory at the high temperatures described, having high enough heat conductivity to be able to transfer heat from its interstices to the surface of the heating element for balancing the rather rapid removal of heat by the hydrocarbon material,

Fig. 1 is a semi-diagrammatic side elevation view of one form of apparatus which might be employed for carrying out our invention.

Referring to Fig. 1, 2 represents the unit in' which heating and processing operations may be carried out. The entire unit may be constructed of steel, ceramic work and insulating materials. The interior of this unit is comprised of the cracking or pyrolysis assembly 3 and combustion chamber 4. The combustion chamber communicates with part 3 by means of the throat 6. By this construction and by our novel operation, as will be described in detail hereinafter, we are able to prevent overcracking because of the hydrocarbon gases being processed coming into contact with refractory surfaces heated to extremely high temperatures, as of necessity in the vicinity of the burners.

The combustion chamber is equipped with one or more units 1, for supplying heat thereto. These units may more or less comprise a structure the same or similar to conventional liquid or gaseous fuel burners. For example, a source of combustion air is provided ,at 8 and a source of fuel at 3. These conduits may be, if desired, connected with proheaters but such is not necessary in our construction. In addition, the construction is provided with a conduit I l for introducing steam or other purging medium into the apparatus. All of the aforementioned parts would be equipped, preferably, with automaticsynchronized valves. However, manually operated equipment may be employed.

The lower portion of the unit is connected by valved conduit l2 to a stack IS. The lower portion is also connected by conduit 14 to sources of diluent l8 and gas I! for processing to acetylene.

Intermediate of the unit are provided a plurality of gas passageways it of a particular construction. These passageways should be constructed so that there are definite relationships between the surface of the passageway to the volume thereof, as well as other relationships. That is, forexample, the ratio of the surface of any one of these passageways expressed in square feet to the volume of the passageway expressed in cubic feet should be greater than 30. The ratio of the cross section area of any one of said passageways to the area of refractory surface should be less than 0.01. As indicated above, our construction is considerably difi'erent from the construction employed in gas making or carbon black regenerative furnaces. For example, where in ordinary regenerative practice the ratio of slot thickness to refractory thickness, taken on horizontal section, is approximately 1:1, we have found that a 1:3 to 1:6 ratio (as will be discussed in detail under Figs. 3, 4 and 5) is required in acetylene production. The passageways are constructed from refractory brick, as for example silicon carbide bricks laid up in long narrow passageways of any desired width. For example, the passageways might be 15-30 feet long, several feet wide, and a fraction of an inch thick. indicated. silicon carbide bricks or slabs are preferred. Our preferred checkerwork is built of split bricks, which is a brick not greater than 1% inches in thickness, laid on edge with slots V4" the reaction products may be withdrawn through asiaeea I a derstood that suitable inlets (not shown) for conduit 22- to a quenching device 23. For best results, the header Should be as restricted in volume as possible, thereby differing from usual regenerative furnaces in this respect. For example, we prefer to'construct the header in our apparatus of such arestricted volume that the velocity of the cracked gas mixture passing through the header is at least 5,000 ft. per minute. In acetylene production the use of such a restricted header is desirable to shorten the time the gases remain at high temperaturebefore being quenched.

This quenching device comprises the liquid seal box 24 partLv filled with -a quenching medium such as water, introduced through pipe 25. Suitable overflow mechanism and valve may be provided at 26 and 21. The oiftake conduit 2| for the acetylene-containing gases produced may be connected with various equipment as described in Hasche Patents 2,236,534 and 2,236,535, or in the several Wulfi' Patents 1,843,965, 1,880,308. and 1,880,309. c The construction shown in Fig. 2 is in'many respects similar to that already described with respect to Fig. 1. In the arrangement of Fig. 2, the combustion chamber 4| is independent of the processing unit 42. However, the combustion chamber is positioned adiacent'and connected to the processing chamber by means of the passageway 43, comparable to some extent to the throat. 8 g. 1). Processing chamber 42 is provided with the elongated slot construction 44, the same as described with respect to Fig. 1. That is,'the ratios of slot thickness to refractory thickness, area ratios and other construction, is exactly comparable to that described. For satisfactory operating conditions, it is highly desirable that the construction of these slots, in which the hydrocarbon gases become pyrolyzed, be fabricated with considerable care and in accordance with the novel arrangement we have disclosed, and as well be considered in further detail hereinafter.

The lower portion of unit 42 is provided with conduit 46 leading to the stack and inlet 41 for the materials to be processed. The outlet chamber 43 is connected by conduit 49 to quenching device 5|, similar to that already described with respect to Fig. 1. Part 45 comprises an opening for inspection of the top of the checker which also serves as a means for obtaining temperature and for gas sampling,

As already indicated, passageway 43 connects the pyrolysis chamber to the combustion chamber 52. A starting stack is provided at 53 and the remainder of the construction may be in accordance with whether oil, gas or other type of fuel is to be burned for furnishing heat to chamber 42. Igniting checkers 54 and other similar elements may be included. It is, of course, un-

. o a hence, for computations we have found that it is I ard materials. In the event of an irregular confuel and air would lead to the combustion chamber.

a It is also understood that our apparatus may be equipped with flow meters. pyrometcrs or various other measuring or recording devices for assisting in the operation thereof.

Referring now in particular to=-Figs. 3, 4, and 5,

additional explanationwill be set forth respecting the ratio of the slot area to the area of refractory on any cross section through the cracking chamber. An understanding ofour novel ratios is apparent to a substantial extent from the construction of the legends appearing on the drawings where the various dimensions of thickness of refractory, thickness of slot (or passageway) and widths thereof have been indicated.

While we have indicated in Figs. 3 and 4 that the external configuration of our apparatus may be circular or rectangular, in general the exact external configuration is not a limitation upon our invention. That is, the shape of our apparatus may be regular or irregular as may be desired. We usually employ a regular construction inasmuch as this lends itself to easier construction with standard split bricks and other standstruction where there are slots of varying widths it also generally follows that the width of the re-' fractory will vary in a comparable manner;

satisfactory to usually consider the average width of the slots and refractory the same. Hence, with this in 'mind, although we may refer to the ratio existing between the slot or passageway area and the refractory area, their ratio may resolve itself to one between the thickness Q of the slot and the thickness of the refractory Also, the range of the ratio, namely 1:3 to 1:6, provides latitude for irregular configurations.

-The ratio as respects numerical dimension,

therefore, is between the V to y -inch thickness of'the slot as designated on Fig. 5 as passageways or as It in Fig. 1, or as 44 in Fig. 2, and

the maximum lye-inch thickness of the refractory. Since the width. as indicated,,may'-be considered theme for both slots and refractory, the ratio of the slot area to the refractory area on any cross section would likewise fall within the range of 1:3 to 1:6. In other words, the refractory is three times as thick as the slot and may be six times as thick as the slot. An example of the latter instance is where a l /z-inch thick refractoryis employed with a A-inch slot. The lower limit'of the thickness of the refractory is, of course, governed by the aforesaid ratios, but the limit on'this lower dimension is not as important, a factor as the mateiy 1% inches. That a maximum of 1 inches. as specified, should be employed has been discovered by us after extensive investigation as being a factor certain constructions, were attempted for use un-- der the rate of heat withdrawal and other conditions encountered in acetylene manufacture,

specification that the thickness of the refractory not exceed approxiour processes involving through conduit ll.

spalling or other thermal deterioration of the refractory takes place. While constructions involving refractory several inches thick may be satis factory for low temperature processes, we have found that such constructions are unsuitable for the high temperatures and high rates with which the process and apparatus of the present invention are concerned.

In our construction, however, we have-found. that the thickness of the refractory being within theratio of 1:3 to 1:6 aforesaid, that is, three to refractory thickness not greater than approximately 1 inches, satisfactory results may be obtained.

The operation of our apparatus, as well as a better understanding of our novel process for producing acetylene, may be had from the con; sideration of the following examples, which are embodiments of our invention. Assuming the process is to be carried out in apparatus such as shown in Fig. l, the valves in the lines l6 and I1 gases pass through the throat i into contact with the elongated slots, thereby heating the refractory bricks defining said slots. By. our construction, it is possible to transfer 80-85% of the combustion heat to the refractory, the exit gases escaping tothe stack. At the expiration of two or three minutes, depending upon the size of the equipment, rate of combustion and other factors, the heating is discontinued and steam introduced In a short time, as a few seconds, this steam sweeps all of the combustion products out of the chamber and into the stack.

Thereafter the stack valve is closed.

Immediately thereafter hydrocarbons to be processed and diluents. such as steam, are admitted through lines I6 and i1 and pass into chamber it. From thence the mixture to be processed passes up through the elongated slots which have been previously described and become heated to a temperature, in this example, of approximately 1250-l350 C. and pass into chamber 2|.

The steam purge previously referred to has during this time been continued and flows through throat 6 becoming intimately mixed with the. acetylene containing gases at 2|. While not essential, this use of steam may be desirable because it prevents the gas being processed from entering the combustion chamber or otherwise contacting such parts and thereby becoming overcracked. At the same time the steam increases the velocity of the cracked mixture in its passage through conduit 22 and into the quencher 23. The valve 21 having been previously opened, permits the cracked gas to become quenched by flowing through the liquid in the quencher, thereby dropping the temperature to below 400' C. Thereafter, the acetylene containing gases are withdrawn through conduit It to a gas holder or otherequipment.

In the operation of ourprocess, the hydrocarhon-containing material, such as butane and steam diluent, is passed through the elongated slots II at a rate of flow greater than 10 pounds of hydrocarbon per minute per square foot of cross sectional area'of slots, but less than approximately 100 pounds per minute. As previously indicated, the slots are not greater than inch in width. The length of the slots may be 15 feet or they may be longer, as for example 30 feet. Usually the -inch thickness of slot would be employed when the slots are 25 or feet long. By such procedure and by the use of the elongated slot construction described, the hydrocarbon completes its passage through theslots in a fraction of a second, yet in this small period of time is capable of taking up from the refractory sufilcient heat to raise its temperature and crack it to an acetylene-containing gas. The gas being process ed preferably contains a diluent such as steam and in addition, as already indicated, when the eprocessed gas emerges into chamber 2|, it may become further mixed with steam flowing through 'the conduit 6. This steam purge, if employed,

, during the cycle helps conduct the oil. gas to the set forth primarily for-illustrating the preferred 30 quenching device and to prevent unnecessary eddies into the combustion chamber.

The gas removed through conduit 2|! may contain 14l6% acetylene. After the process has been in operation a minute or so, the temperature of the silicon carbide bricks will have dropped somewhat and the quantity of acetylene being produced may also drop. At this point, the processing cycle may be stopped by closing first the valve in line l1 and shortly thereafter the valve in the diluent line I. Valve 21 would be closed and the stack valve open. The steam through conduit II is discontinued and air introduced through conduit I. This air burns out any carbon accumulating in the elongated slots. A short time thereafter, fuel is introduced through conduit 9 and the heating cycle starts and is operated for a few minutes until the refractory has again obtained the desired temperature.

By automatic operation and synchronization of the valves, the heating and processing cycle operated as described, thereby obtaining a continuous type process. By employing cycles of a few minutes each, the quantity of acetylene produced is generally above 10%, particularly when saturated hydrocarbons as propane, butane, pentane, and the like are the hydrocarbons processed. However, the various hydrocarbons and diluents listed in the aforementioned Wulif patents. Hasche Patents 2,236,534 and 2,236,535, and other prior art, may be treated; hence, extended comment herein is unnecessary.

Referring to Fig. 2, the operation and construction of this modified unit is similar in many respects to that already described. In this unit the heating in chamber 4| would be operated alternately with the processing in chamber 42. The heating chamber 4| would be started up and oil gas or other fuel capable of producing a high tem: perature introduced therein to obtain temperatures, for example. in excess of 1600" C. The hot combustion products are conducted through the throat 43, the passageways M and out the stack conduit 45. During this cycle the valve at the end of conduit 49 would, of course, be closed.

At the conclusion of the heating step the hythe changing of the valves a few seconds and the heating cycle three to five minutes. As already indicated, preferably prior to" the starting of the heating cycle, after the completion of the cracking cycle some air would be introduced for a few seconds, thereby burning out any carbon from the elongated slots. Thereafter, the fuel supply would be started and hot combustion productsproduced in the combustion chamber. The completely burned products flowing through the elongated slots passageways, quickly and readily heat the refractory work to the high temperature specified. As a matter of fact, the gases going to the stack are at a relatively moderate temperature, the greater portion of the heat having been removed therefrom in the refractory work.

As pointed out, in our construction the slot refractory ratio is considerably different from that in regenerative units used for hydrogen and/or carbon black production, the heat is readily given up at a high rate to the materials being processed and by this high rate of heat transfer the hydrocarbon becomes decomposed to a gas containing acetylene, ethylene and other constituents. For example, from our process a gas containing 12%-16% acetylene and 5%-25% ethylene may be readily obtained.

When cracking butane with an 8:1 volume. ratio of steam to hydrocarbon and employing a cracking cycle of 1 minutes duration, following are analyses of cracked gas obtained in percent by volume:

After 15 After 90 3 secs. Secs. cycle The steam purge and other elements already described with respect to Fig. 1, may likewise be employed when operating the process in Fig. 2. For example, if desired, steam may be introduced near throat 43, or a valve may be inserted in this passageway. However, by the particular construction shown in Fig. 2, .chance of overcracking, due to contact with combustion chamber parts, is, m ed, and such features may be omitted.

The following specific data will illustrate in further detail the high rate of heat transfer obtainable in our novel process and apparatus for acetylene manufacture. In the furnace from which the following data was taken, the portion of the elongated slots at a temperature above 700 C. was approximately 7 feet. Theslots constituted relatively straight narrow, unobstructed passageways as apparent from the drawj subtracted the heat in the combustion products atapproximately 900 C., the temperature of the gas leaving the hot zone (approxi ponderance .portant factor.

ings. The other dimensions of the heating passageways fell within the ratios already described in detail, hence, further description thereof is unnecessary. The refractory boundingthesiota 1 in this example were constructed of the refractory y commercially known asfcarborundumfl The cracking cycle was of conditions Average'refractory temperature,1bottonrofreac tion zone, '700--C.' Averagerefractory te zone, 1400 C.-

Avgerage gas temperature, bottom of reaction zohcf v 0 00 C. 7 Average gas temperature, leaving cracking zone,

Logmean temperature diiference,'159 C.

Butane cracked-15.5 C. F. v Steam dilution, 300 C. F.

.Sensible and reaction heat of butane and. steam,

Surface of Carborundum exposed .in ireactionj zone, 39.4 sq. ft. V Effective thickness of Carborundum checkers from surface to'center,'0.315 in. (thisrepresents 7' an average amountin to approximatelyonc quarter of a split brick) Fromthese data, the heattransfer in t. u.s/ inch/square foot/degree Fahrenheit/hour can be A calculated as follows:

The figure of 41.8 B. t. u. is, of course, an average" figure for the entire cracking zone. It would be in our novel process and regenerative apparatus for converting hydrocarbons to acetyleneis not the resistance of hydrocarbon gas film, but is to a large extent the conductivityof' the refractory itself (in this instance Carborundum) Although radiation plays an important role, the

radiated.

As' indicated, the heating cycle lasts abouttwice as long as the cracking cycle. Likewise, the

heating conductivity-of the refractory is an im-' During our heating cycle there was burned 17.9 C. F. of butane which theoretically liberates 58,000 B. t. u. From this may be a temperature of mately 19,000 B. t. u.) This gives 39,000 B. t. u.,

which satisfactorily corresponds to the heat transferred in the cracking cycle, (37,200 B. t. u.)

It is, therefore, apparent that our process and In the aforemenheating elements appr ximately l /g'minutes 7 duration, the heatingflcyclebei g roughlytwlce the cracking; The following-were the-operating heat must be transferred to the surface before it can be be over about C. or 200 C.

apparatus is susceptible of some modification. However, it is to be observed that for preferred operation the ratios respecting surface of heating refractory, the mass of heating refractory, and quantity of hydrocarbons fed are somewhat critical and should be followed in accordance with our disclosure herein.

Space velocity for the purpose of this applicapassageway by its length (i. e. height in figures shown) would be employed. Otherwise, when computing volume, the dimensions, height, width and thickness of the passageway would be employed.

When computing the areas on a cross section, the width times the thickness of the slot or'the refractory, as the case might be, would be employed. In most instances, since the width may be considered as unity since it is the same as for both the slot and refractory, the ratios may be observed directly from a comparison of the respective thicknesses. I

We prefer to employ a refractory such as silicon carbide, bricks as a standard commercially obtainable brick, such as Carborundum." However, other refractory materials that possess a heat conductivity comparable to and not less than about 75% that of Carborundum might be substituted in all or in part in the construction of the vertical elongated slots that comprise our apparatus. as the hydrocarbon cracked, any of the various other hydrocarbons, both aliphatic and aromatic, gaseous or liquid, as described in the aforesaid Hasche patents, or the several Wulff patents referred to herein, may be processed in accordance We have found that the space While we have described butane with the invention described herein. Likewise,

any of the various diluents may beemployed.

It can be seen from the foregoing that our apparatus is particularly advantageous since it will withstand a high rate of heat withdrawal, sumcient to crack hydrocarbons to acetylene, and high temperatures. It is apparent that since our apparatus will operate under the critical conditions of producing acetylene and withstand thermal conditions encountered, that our apparatus will readily withstand the less drastic conditions encountered in other types of processes where less exacting conditions are required such as the heating of gases in connection with steel annealing or the heating of organic materials to produce ethylene, or the heating of other organic materials.

What we claim and desire to be secured by Let- 'ters Patent of the United States is:

paratus, of slot to area of refractory being be-.

gated passageways several feet long and wide.

but only V to inch thick, the ratio of the slot area to the refractory area on a cross-section through the cracking chamber being from 1:3 to 1:14, the ratio of the surface of any one of the passageways expressed in square feet to the volume of the passageway expressed in cubic feet being greater than 30, and means for supplying said material to -and withdrawing heated materials from the apparatus, associated therewith.

3. An apparatus for converting hydrocarbons to acetylene comprising a unit including a combustion chamber and a processing chamber, means connecting said chambers, said processing chamber containing a plurality of silicon carbide refractory members not greater than one and one-half inches thick, positioned therein to form a plurality of elongated slot passageways at least 7 feet long but only Y to -inch thick, the ratio of slot to refractory on a cross section through the processing chamber being between 1:3 to 1:6, the ratio of the area of the silicon carbide surface of any one of said passageways to the volume thereof expressed in cubic feet being greater than 30, and conduits for'feeding said hydrocarbons to and withdrawing the acetylene formed in the processing chamber, associated with the apparatus.

4. An apparatus for heating gases'to high temperatures in excess of 1100 C. with high rate of heat withdrawal, comprising a housing, said housing containing a plurality of silicon carbide brick members of a thickness not greater than one and one-half inches, said members thickness thereby being such that destructive spalling does not occur at said high temperatures and rate of heat withdrawal, said silicon carbide members being positioned to form a plurality of unobstructed slot passageways more than approximately 7% feet long, and to /2 inch thick, the ratio of the area of passageway on a cross section to area of refractory being from 1:3 to 1:6, the

' ratio of the silicon carbide surface of any one of said passageways expressed in square feet to the volume thereof expressed in cubic feet being greater than 30, conduit means leading to the apparatus for supplying said gases thereto, and other conduit means for withdrawing heated gases therefrom, associated with the apparatus.

5. In an apparatus of the class described, a housing, a plurality of silicon carbide refractory members not greater than one and one-half inches thick positioned within the housing to form a plurality of elongated, substantially unobstructed passageways to -inch thick, approximately 7 2 to 30 feet long and several feet wide. the construction being characterized in that on at least substantially the major part of any cross section of a section across the aforesaid refractory and slots, the refractory thickness'with respect to the passageway thickness will be not less than three times and not greater than six times said obstructed passageways A- to /2-inch thick, ap-

proximately 7 to 30 feet long and several feet wide. the construction being characterized in that on at least substantially the major part of any cross section of a section across the aforesaid refractory and slots, the refractory thickness with respect to the passageway thickness will be not less than three times and not greater than six times said passageway thickness, the ratio of the surface of any one of the passageways expressed in square feet to the volume of the passageway expressed in cubic feet being greater than 30, and means for supplying materials to said passageways and withdrawing heated materials therefrom, associated with said apparatus.

RUDOLPH LEONARD HASCHE. WILLIAM B. HINCKE. 

